CA1286325C - Hazardous waste reactor system - Google Patents
Hazardous waste reactor systemInfo
- Publication number
- CA1286325C CA1286325C CA000545997A CA545997A CA1286325C CA 1286325 C CA1286325 C CA 1286325C CA 000545997 A CA000545997 A CA 000545997A CA 545997 A CA545997 A CA 545997A CA 1286325 C CA1286325 C CA 1286325C
- Authority
- CA
- Canada
- Prior art keywords
- reaction zone
- organic compounds
- water
- gaseous mixture
- zone
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Lifetime
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
- F23G5/10—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating electric
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/72—Organic compounds not provided for in groups B01D53/48 - B01D53/70, e.g. hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/243—Tubular reactors spirally, concentrically or zigzag wound
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00026—Controlling or regulating the heat exchange system
- B01J2208/00035—Controlling or regulating the heat exchange system involving measured parameters
- B01J2208/00044—Temperature measurement
- B01J2208/00061—Temperature measurement of the reactants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00389—Controlling the temperature using electric heating or cooling elements
- B01J2208/00415—Controlling the temperature using electric heating or cooling elements electric resistance heaters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00477—Controlling the temperature by thermal insulation means
- B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00513—Controlling the temperature using inert heat absorbing solids in the bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/0061—Controlling the level
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S588/00—Hazardous or toxic waste destruction or containment
- Y10S588/90—Apparatus
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Health & Medical Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Biomedical Technology (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- Materials Engineering (AREA)
- General Health & Medical Sciences (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- General Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Processing Of Solid Wastes (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Treating Waste Gases (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Refuse Collection And Transfer (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Micro-Organisms Or Cultivation Processes Thereof (AREA)
Abstract
HAZARDOUS WASTE REACTOR SYSTEM
ABSTRACT
A method and reactor system are described for decomposing organic compounds. A gaseous mixture of organic compounds and water, equal to or in excess of stoichiometry, is passed into a first reaction zone having a temperature range between about 200°C and 1400°C. The first reaction zone has a labyrinthine path which presents organically adsorbent surfaces to the gaseous mixture to provide a residence time in the first reaction zone sufficient to react substantially all of the gaseous organic compounds and the water at high rate. The effluent from the first reaction zone, still with water equal to or in excess of stoichiometry, is then passed to a second reaction zone having a temperature range between about 750°C and 1820°C to decompose the organic compounds remaining in the effluent. The first reaction zone is an annulus which is coaxial with and surrounds the second reaction zone. The labyrinthine path is formed by particulate ceramic material.
ABSTRACT
A method and reactor system are described for decomposing organic compounds. A gaseous mixture of organic compounds and water, equal to or in excess of stoichiometry, is passed into a first reaction zone having a temperature range between about 200°C and 1400°C. The first reaction zone has a labyrinthine path which presents organically adsorbent surfaces to the gaseous mixture to provide a residence time in the first reaction zone sufficient to react substantially all of the gaseous organic compounds and the water at high rate. The effluent from the first reaction zone, still with water equal to or in excess of stoichiometry, is then passed to a second reaction zone having a temperature range between about 750°C and 1820°C to decompose the organic compounds remaining in the effluent. The first reaction zone is an annulus which is coaxial with and surrounds the second reaction zone. The labyrinthine path is formed by particulate ceramic material.
Description
~2~363;25 HAZARDQUS WASTE REACTOR SYST~M
This invention relates generally to the decomposition of organic compounds, such as toxic waste products. More particularly, the invention relates to an improved method and reactor system for decomposing organic compo unds. - -various types of high temperature reactors are employed in the processing of organic compounds, such as toxic waste materials, to convert such materials into compounds which are more acceptable for discharge into the environment or in some cases, re-use. The various processes employed in such reactors include pyrolysis, thermolysis, disassociation, decomposition, and combustion.
Prior art mêthods and apparatus for decomposing organic compounds have suffered from a number of significant problems with respect to both the processing and the structural aspects of the particular technology employed. For example, many prior art reactor systems provide a relatively short residence time of the reactants within the reaction zone. As a result, it has become necessary in such reactors to employ very high temperatures and/or pressures to completely react the products being processed. ~igh temperatures create many problems with respect to the reactor structural elements, since they may become weakened or reactive at the high temperatures employed.
Moreover, the energy requirements in such systems often result in relatively high operating cost.
The need for processing large amounts of organic material has often, in prior art technologies, required the construction of very large reactor systems. The expense and relative unwieldiness of such , .
: ." . , .
.
.. . . .
.
- . .
- - ~ . . :
.
.
lZ8~ 'S
large scale reactor Systems has made them undesirable ~or many applications.
It is an object of the present invention to p{ovide an improved method and reacto~ system for decomposing organic compounds.
Another object of the invention is to provide a method and reactor system for decomposing organic compounds wherein a proper combination of temperature, turbulence and residence time in reaction is provided for the compositions being processed.
Another object of the invention is to provide a method and reactor system for decomposing organic compounds which are opera~le at slightly below atmospheric pressure and at high heating ef~iciency.
It is a further object of the invention to provide a method and reactor system for decomposing organic compounds that have a high throughput capacity relative to the ~equired size of the reactor system.
A still further object of the invention is to provide an improved method and reactor system for decomposing organic waste which are capable of processing toxic waste materials into harmless compounds under relatively safe and controllable conditions.
Other objects of the invention will become apparent to those skilled in the art from the following description, taken in connection with the accompanying drawings wherein;
FIGURE 1 is a schematic diagram of a reactor system incorporating the invention;
FIGURE 2 is an enlarged cross-sectional schematic view of the reactor or thermolytic detoxifier portion of the reactor system of FIGURE 1; and FIGURE 3 is a graph illustrating a typical set of process conditions during the decomposition of one representative class of organic compounds in accordance 28~ 325 with the invention.
Very generally, the invention decomposes organic compounds by passing a mixture of the organic compounds and water in a gaseous form into a reactor having at least one reaction zone which has a temperature range between about 750C and about 1820~C to decompose the organic compounds.
The amount of water is controlled to provide an excess of stoichiometry.
Referring now more particularly to the method Of the invention, the present invention differs from methods most commonly employed by the prior art in connection with the decomposition of organic compounds.
Unlike mo~t prior art techniques, the present invention employs wate~ in exces~ o~ stoichiometry in the teact$on to cause a disassociation reaction of the organic compound with the water to form carbon dioxide, carbon monoxide and hydrogen. Most prior art reactions are based upon a flame combustion reaction in which the organic compound i~ mixed with a fuel to be burned, at high temperature, with air ~oxygen) to produce carbon dioxide and water. The problem with the latter type of reaction i9, in addition to re~uiring high temperature and high heat removal, the reaction may produce undesirable side reactions and recombinations ~products of incomplete combustion or ~ICS) which could result in P~
: , .
.
.:
.
- . .
~ ~ .
~Z8fà325 the release of toxic compounds into the environment with the effluent.
A benefit of the type of reaction employed in accordance with the method of the invention is that the - reaction is endothermic. This provides stability and safety ~ince heat is not released from the reac~ion and therefore the structural parts of the reactor are maintained at a lower temperature than they would be if the reaction were exothermic, as is the case with the combustion method. If desired, the method of the invention may be run concurrently with some oxidation reaction by adding air and/or oxygen to the input gaseous ~ixture. By regulating the amount of air introduced, it is possible to run the method as e8sentially thermally neutral.
In the ~llustrated embodiment, the gaseous mixture passed to a first reaction zone into which the gaseous mixture of organic compounds and water is passed i8 maintained at a temperature range between about 200C
and 1400C. The low temperature of the range will depend upon the temperature of the gases as they are introduced to the first reaction zone. The high temperature of the range will depend upon the reactor structure itself and the thermal limitations of the structural components. With the first reaction zone comprising an annulus which is, as will be explained below, heated from the interior thereof, the amount of heat radiated and convected from the outer surfaces of the first reaction zone will affect the temperature range of it8 operation. In the preferred embodiment, the first reaction zone is a folded annulus in which the gases flow first downwardly in the outer part and then upwardly in the coaxial inner part.
ln accordance with the invention, the first reaction zone has a labryinthine path which presents organically adsorbent surfaces to the gaseous mixture ~owing through the lab,y~ntbine path. By orgAn-callY
- '' ~Z863~:5 ads~rbent surfaces, it is meant surfaces which adsorb the organic gaseous compounds flowing through the first reaction zone, thereby slowing their flow rate and enhancing their kinetics by retaining such compounds in the zone to be fully reacted therein. By employing a labryinthine path, namely, a path that produces a tortuous and highly turbulent flow to the gases passing therethrough, sufficient mixing of the gases and therefore sufficient exposure of the organic compounds therein to the adsorbent surfaces are assured.
In accordance with the present invention, the labryinthine path and the adsorbent surfaces are selected to provide sufficient temperature, turbulent mixing, and residence time in the first reaction zone for substantially all of the gaseous organic compounds to react with the water within the first reaction zone.
By substantially all of the organic compounds, it is meant in excess of 99% and preferably in excess of 99.99% reacted. Preferably, to ensure proper turbulence and surface area, the void volume in the first reaction zone is selected to be between about 30~
and about gO~ of the total volume of the first reaction zone. Preferably, the void volume is about 75% of the total volume. As will be explained below, the void volume and tortuous path are provided by ~electing particulate material having a shape suitable to provide the above-stated characteristics.
In order to assure that the products in the first reaction zone are substantially all reacted, the amount of water added to the gaseous mixture is equal to or in excess of stoichiometry. By this terminology, it is meant that mole for mole, the amount of water is greater than is necessary to combine with 100% of the organic compounds present in the gaseous mixture. ~he preferred range is between 100% and 200% of stoichiometry, since anything greater than 200% has a ~''' ' ` '' '' ': '' ~Z86325 tendency to reduce the operating temperatures undesirably. The optimal percentage has been found to be about 131% of stoichiometry, namely, 31% in excess of stoichiometry. These levels of water assure the desired substantial reaction of the organic compounds and C02 formation in the first reaction zone, while maintaining optimal temperatures~
After reaction in the first reaction zone, the effluent from the first reaction zone is passed to a second reaction zone for further reaction. The temperature of the second reaction zone is at a higher temperature than that of the first, having a temperature range between about 750C and about 1820C.
In the second reaction zone, the rem~ining organic compounds are decomposed to carbon dioxide, carbon monoxide and hydrogen. If any oxygen is added to the gas mixture, the reaction products will also include water. As was the case in the first reaction zone, the amount of water in the second reaction zone is controlled so that it is equal to or in excess of stoichiometry in the second reaction zone. The higher temperature of the second reaction zone, together with the relatively low level of organic compounds entering the second reaction zone, assure that total and complete reaction of the organic compounds results to a level of at least 99.99~ and typically much higher.
To further assure complete reaction, the residence time of the gases in the second reaction zone is made about equal to the residence time in the first reaction zone. To do this, the flow cross-section of the second reaction zone may be made substantially larger than that of the first reaction zone to thereby increase the residence time of the flowing gases.
Preferably, the flow cross-section of the second reaction zone is about twice that of the first.
In accordance with the invention, heat is ~2~325 introduced to the reactor directly to the second reaction zone. The first reaction zone is an annulus which is positioned adjacent the second reaction zone coaxially thereof and surrounding same. AS a consequence, the heat in the second reaction zone is radiated and conducted to the first reaction zo~e to provide heating thereof.
The flow rate of the gaseous mixture introduced to the first reaction zone is, preferrably, between about two kilograms per minute and about eight kilograms per minute. The precise flow rate of the organic compound versus the water and/or oxygen will, of course, be determine~ by the stoichiometry of the chemistry involved. The flow rate of the gaseous mixture introduced to the first reaction zone is, preferrably, between about l9 cubic meters per minute and about 3.5 cubic meters per minute, depending upon the particular compound being decomposed. Typically, for a given temperature, the larger the molecule, the longer the reaction time and the higher the temperature needed to effect the desired reaction.
Referring now to FIGURE l, a typical configuration of a reactor system incorporating the invention is shown. In the system of FIGURE l, a plurality of metal drums ll, 12, 13 and 14 are shown connected to the system. It is to be understood, however, that the system of the invention and the method of the invention may be utilized in connection with a single drum or other container or source of organic materials to be decomposed, or a plurality of such sources. As shown in ~IGURE l, each drum is connected via a bidirectional flow coaxial conduit 16, 17, 18, and l9, respectively to the thermolytic detoxifier described in detail below. Each conduit has a central duct and an outer duct of annular cross section extending coaxially and coextensively with the ,' .
- ~ , . .
128~3 ~5 central duct. Flow into the respectiVe d~ums is provided through connectors 21 whereas outflow from the drums is provided through connectors 23. Outflow from the drum~ is carried through the coaxial conduits 16-19 in the inner duct of the condui,, whereas flow of hot steam and gases into the drums is through the outer annular cross-section duct of the conduit. An extension 25 is provided to couple the outer duct of the coaxial conduits 16, 17, 18, and 19 to the connectors 21. The inner ducts couple to the connectors 23.
The opposite ends of the conduits 16-19 ~rom the drums 11-14 have their central ducts all connected to an inlet conduit 27 via an extension 29. A duct 31 is connected to the outer duct of each of the coaxial conduits 16-l9 for reasons explained below. A no~mally closed valve 33 separates the inlet conduit 27 from the duct 31.
In order to volatilize the contents of the drums 11-14, the drums are heated by any suitable means. In the illustrated embodiment, a resistive heater having a plurality of coils 35 is shown surrounding the drum 11. The heater 35, together with the hot gases flowing back to the drum, raises the temperature of the drum contents to the desired level.
Similar heaters, not shown, may be provided for the other drums. Volatilization of the contents of the drums, together with the action of a turbine blower, described below, causes passage of the volatilized contents through the central duct of the conduits 16-19 through the extension 29 to the inlet conduit 27.
Water is mixed with the volatilized contents of the drums 11-14 by steam in the gas flow to and from the drums. The steam is present as a result of water addition to the reactor detoxifier 45, explained below.
The steam thus formed passes back through the outer 128~325 g annulus in each of the conduits 16-l9, depending upon the drum being operated, to pass into the drum in the space above the o~ganic material therein. In this space, the steam is mixed with the volatilized organic material and passes up through the central duct of the coaxial conduit 16, through the extension 29 and the conduit 27 and into the reactor or thermolytic detoxifier 45. ~y using the illustrated coaxial conduit arrangement, the walls of the central duct, carrying the volatilized organic compound from the drum, are kept hot enough to prevent condensation, carbonization, precipitation, and crystallization, which could plug the duct.
The internal structure of the thermol~tic detoxifier 45 is discussed in detail below. The effluent from the thermolytic detoxifier 45 passes through an outlet assembly 47 into a conduit 49. A
safety burst disk 51, designed to rupture upon the pressure of the conduit 49 exceeding a predetermined safety level, is interposed in a duct 53 communicating between the outlet 47 and a vent tube 55. The duct 49 communicates from the outlet 47 of the thermolytic detoxifier 45 to the gas-to-gas heat exchanger 43. The outlet assembly 47 can include an internal cyclone separator (not shown) to remove any fine dust carried out of thermolytic detoxifier 45.
The gas-to-gas heat exchanger 43 may be of any suitable design which serves to exchange heat from gas flowing out of the thermolytic detoxifier 45 to gas flowing into the conduit 40. After exchanging heat with such gas, the effluent passing from the conduit 49 through the gas-to-gas heat exchange~ 43 enters a conduit 57 which leads to a sorber tower 59 of suitable construction. The sorber tower 59 contains a suitable sorbent material for adsorbing any remaining impurities flowing through the conduit 57.
lZ86325 A cond~it 61 returns the effluent from the sorber tower 59 to a turbine blower 63 which provides the main motive force for producing flow in the ill~strate~ system. The outlet of the turbine blower 63 passes through a conduit 65 and through a control valve 67 into the gas-to-gas heat exchanger 43 where it is heated by the gas from the conduit 49. A normally closed valve 69 provides for venting the output of the sorber tower 59 through the turbine blower 63 via the vent 55. A pressure gauge 71 is connected to monitor the pressure across the sorber tower 59.
In order to introduce the necessary amount of water to the reactor, a water conduit 41 is provided connecting a pressurized source 37 of water to a steam inlet port 44 on the thermolytic detoxifier 45. Water flowing through the conduit 41 is heated to form steam in the coiled regions 76 and 77 of the conduit 41.
These coiled regions are formed around the conduits 57 and 61 through which the hot effluent from the thermolytic detoxifier 45 flows. Further capture of heat for the water flowing through the conduit 41 is accomplished by a plurality of coils 78 which are wrapped around the outer surface of the thermolytic detoxifier 45. Thus, by the time the water enters the thermolytic detoxifier 45 via the port 44, it is heated to the form of superheated steam and mingled with the gases entering the thermolytic detoxifier via the inlet conduit 27.
Control over the process is provided by a suitable control processor 73. Control processors utilizing various types of computers are well known in the art and therefore the control processor 73 will not be further described in detail. The operation of the control processor 73 is controlled from a suitable computer monitor 75 and touchscreen.
In operating the system illustrated in FIGURE
J2~3632S
1, each of the drums 11-14 is connected, one at a time, through the respective conduits 1~-19 to the system.
Each drum may be associated with a suitable identification code reading system, and a suitable interlock, not shown, may be used to assure that the drum may not be connected to the system until its contents are properly inputted to the control processor 73 and approved for processing.
Referring now to FIGURE 2, the specific internal details of the reactor or thermolytic detoxifier 45 may be seen in cross-section. The thermolytic detoxifier 45 comprises an outer cylindrical wall 73 of a material having sufficient structural strength at the relatively high operating temperatures described above to maintain the integrity of the reactor. Preferably, the material is type 316-L
stainless steel tubing having a thickness of four to eight millimeters wherein the longitudinal or axial dimension of the thermolytic detoxifier is about 1.8 meters and the inner diameter of the wall is about 43 centimeters. The lower end of the decomposer or reactor is closed by a circular plate 75 which is secured to the cylindrical wall 73 by means of a flange 77 extending from the wall radially outward thereof and by suitable mounting bolts 79. A flange 81 similar to the flange 77 is provided at the upper end of the cylindrical wall 77 and a circular plate 83 is bolted thereto by means of bolts 85. Sandwiched in between the plate 83 and the flange 81 and secured by the bolts 85 is a mounting ring 87. The conduit 27 (FIGURE 1) connects with the interior of the thermolytic detoxifier 45 through a port 89 located near the upper end of the cylindrical wall 73.
Extending from the ring 87 and preferably integral therewith is a cylindrical wall 91. This wall is coaxial with the wall 73 and extends downwardly from ' " ~'' ` ' -12~6325 the ring 87 about 20% of the length of the cylindrical wall 73. Interposed between the cylindrical wall 91 ~nd the cylindrical wall 73 and coaxial therewith is a cylindrical wall 93. The cylindrical wall 93 extends downwardly within the cylindrical wall 73 and terminates a distance above the plate 75 which is between about 5% and 10~ of the total axial length of the cylindrical wall 73. Preferably, the material of the ring 87, the plates 75 and 83, the cylindrical wall 91, and the cylindrical wall 93 is the same as that of the cylindrical wall 73, namely, 316-L stainless steel tubing. For a 1.8 meter length thermolytic detoxifier, the thickness of these latter elements is preferably approximately four to eight millimeters for inner diameters of about 24 centimeters for the wall 91 and 33.9 centimeters for the wall 93.
Supported on the plate 75 and extending upwardly therefrom is a cylindrical wall 95. The cylindrical wall 95 is substantially equal in diameter to the cylindrical wall 91 and is axially aligned therewith. The cylindrical wall 95 is of a length to terminate a distance below the termination of the cylindrical wall 91 so as to leave a space therebetween of a height between about 5% and about 10% of the total length of the cylindrical wall 73. Preferably, the material of which the cylindrical wall 95 is comprised is a cetamic material such as alumina or a mix of alumina and titanium oxide. Mullite (TM) tubing having a wall thickness of approximately one centimeter is a satisfactory material for the cylindrical wall 95 in a reactor of about 1.8 meters length and an inner diameter of the wall 93 of about 33.9 centimeters.
Other suitable ceramic materials for the tubing include Vycor (TM) and Pyroceram (TM).
The result of the foregoing described arrangement is a central reaction chamber 97 which is .
. , . ' .
. . , - .
lZ863Z5 surrounded by a coaxial reaction chamber 99, the latter being separated into two subchambers, an outer subchamber 101 and an inner subchamber 103. Gas entering the reactor through the port 89 may pass downwardly through the outer annulus 101, through the gap between the plate 75 and the lower end of the cylinder 93, upwardly through the inner annulus 103, through the gap between the upper end of the cylindrical wall 95 and the lower end of the cylindrical wall 91, and downwardly through the central reaction chamber 97 to exit through the port 47 in the plate 75.
The annular or outer coaxial reaction chamber 99 comprised of the subchambers 1~1 and 103 is substantially filled with particulate ceramic material indicated at 105. The material is selected to be of a size and configuration to provide a labryinthine path for gas flowing through the outer annulus 101 and inner annulus 103. In addition, the configuration and size Of the material is selected to provide the desired void volume in the space occupied by the material. The material is present in an amount sufficient to extend up to the orifice 89, thus leaving an empty annular plenum 107 at the top of the outer annulus 101 to evenly distribute the flow. Similarly, the amount of material placed in the inner annulus 103 extends to just below the upper edge of the cylindrical wall 95 to leave a plenum 109 at the upper end of the inner annulus 103 the purpose of which is to maintain a cool top flange plate and electrical feedthrough. The ceramic material utilized preferably is in the form of 1/2 inch diameter rashig rings. Also acceptable are spherical or other shaped particles of aluminum oxide.
The materials thereby provide turbulence as well as a large hot surface area exposed to the gas flow to enhance the chemical kinetics and to adsorb and thereby .'~ .
' - ' -1286:~S
increase the residence time of the hydrocarbons in the reaction chamber. This provides the desired kinetics and retention time to effect the reactions described above.
The thermolytic detoxifier 45 is heated by a plurality of elongated U-shaped hairpin shaped loops of electrical resistance heating elements 111. The heating elements 111 extend downwardly within the reaction chamber 97 a distance at least equal to half the length of the reaction chamber. The heaters are mounted in the plate 83 by a ceramic mounting fixture 113. The fixture 113 may be any suitable heat resistant insulation material, for example, quartz, alumina, molybdenum disilicide, lanthanum chromite, and lanthanum diboride. Power for the electrical heaters 111 is provided through electrical feedthroughs 115 mounted to the upper surface of the plate 83. A
radiation shield 116 is also provided just below the fixture 113. Above the heating elements there may be a metal cap (not shown) to provide a good process seal and help reduce further heat loss.
At the bottom of the reaction chamber 97, a volume of particulate material or ceramic structure 117, which can be similar to or identical to the particulate material 105, is provided. The amount of the ceramic material occupies about 5% to 15% of the length of the reaction chamber 97, remaining out of contact with the heating elements 117. The hot gases passing out of the reaction chamber 97 through the vent 47 heat the ceramic material 117. This retained heat is transferred to the ceramic material at the lower end of the annulus 99 for greater heating efficiency thus serving both as a heat recuperator and controlled gas quenching system. The heat within the chamber 97 also heats the cylinder 95 and is radiated and thermally conducted into the ceramic particulate material in the annular reaction zone 99. The flow cross-section of the central reaction chamber is about double that of the annulus 101 and of the annulus 103 to provide the desired residence time.
In operation o~ the thermolytic detoxifier 45, the mixture of gaseous organic compounds and steam (and possibly oxygen) is fed into the reactor through the port 89 and passes downwardly over the material in the outer annulus lOl and back upwardly through the material in the annulus 103. In this region, the hydrocarbons are retained on the hot adsorbent surfaces of the particulate material for a time sufficient to produce the above-descrihed reaction. In addition, the configuration of the particulate material provides sufficient turbulence for adequate mixing and to assure that the organic compounds are brought into contact with the surfaces and with the steam to effect the reaction. The decomposition of the organic compounds is at least about 99% by the time the gas enters the central reactor 97 through the gap between the cylindrical wall 91 and the cylindrical wall 95. In the reactor chamber 97, the gases encounter their highest temperature which then assures complete (at least 99.99%) reaction of the organic compounds, producing the final relatively harmless effluent. The effluent is then passed out of the port 47 for processing as described above.
Referring now to FIGURE 3, a graph depicting temperature variation within the reactor is shown. In addition, the amount of carbon monoxide measured in the source drum is also shown. All parameters measured are graphed with respect to time and for an organic waste consisting of substantially all cyclohexanone.
It may be seen that the temperature in the core or chamber 97 varies from a low of just below 1600F (785C) to a high of about 1850F
(10100C). Temperatures of the outer wall are shown as measured in three different places, a high location at about the level of the gap between the wall 95 and the wall 109, a low level near the lower end of the wall 93, and a mid level approximately half-way between the foregoing two points. Finally, it may be seen that the level of carbon monoxide substantially increases just after beginning operation as the contents of the drum volatilize due to heating. The cazbon monoxide level gradually drops, finally reaching zero after just over
This invention relates generally to the decomposition of organic compounds, such as toxic waste products. More particularly, the invention relates to an improved method and reactor system for decomposing organic compo unds. - -various types of high temperature reactors are employed in the processing of organic compounds, such as toxic waste materials, to convert such materials into compounds which are more acceptable for discharge into the environment or in some cases, re-use. The various processes employed in such reactors include pyrolysis, thermolysis, disassociation, decomposition, and combustion.
Prior art mêthods and apparatus for decomposing organic compounds have suffered from a number of significant problems with respect to both the processing and the structural aspects of the particular technology employed. For example, many prior art reactor systems provide a relatively short residence time of the reactants within the reaction zone. As a result, it has become necessary in such reactors to employ very high temperatures and/or pressures to completely react the products being processed. ~igh temperatures create many problems with respect to the reactor structural elements, since they may become weakened or reactive at the high temperatures employed.
Moreover, the energy requirements in such systems often result in relatively high operating cost.
The need for processing large amounts of organic material has often, in prior art technologies, required the construction of very large reactor systems. The expense and relative unwieldiness of such , .
: ." . , .
.
.. . . .
.
- . .
- - ~ . . :
.
.
lZ8~ 'S
large scale reactor Systems has made them undesirable ~or many applications.
It is an object of the present invention to p{ovide an improved method and reacto~ system for decomposing organic compounds.
Another object of the invention is to provide a method and reactor system for decomposing organic compounds wherein a proper combination of temperature, turbulence and residence time in reaction is provided for the compositions being processed.
Another object of the invention is to provide a method and reactor system for decomposing organic compounds which are opera~le at slightly below atmospheric pressure and at high heating ef~iciency.
It is a further object of the invention to provide a method and reactor system for decomposing organic compounds that have a high throughput capacity relative to the ~equired size of the reactor system.
A still further object of the invention is to provide an improved method and reactor system for decomposing organic waste which are capable of processing toxic waste materials into harmless compounds under relatively safe and controllable conditions.
Other objects of the invention will become apparent to those skilled in the art from the following description, taken in connection with the accompanying drawings wherein;
FIGURE 1 is a schematic diagram of a reactor system incorporating the invention;
FIGURE 2 is an enlarged cross-sectional schematic view of the reactor or thermolytic detoxifier portion of the reactor system of FIGURE 1; and FIGURE 3 is a graph illustrating a typical set of process conditions during the decomposition of one representative class of organic compounds in accordance 28~ 325 with the invention.
Very generally, the invention decomposes organic compounds by passing a mixture of the organic compounds and water in a gaseous form into a reactor having at least one reaction zone which has a temperature range between about 750C and about 1820~C to decompose the organic compounds.
The amount of water is controlled to provide an excess of stoichiometry.
Referring now more particularly to the method Of the invention, the present invention differs from methods most commonly employed by the prior art in connection with the decomposition of organic compounds.
Unlike mo~t prior art techniques, the present invention employs wate~ in exces~ o~ stoichiometry in the teact$on to cause a disassociation reaction of the organic compound with the water to form carbon dioxide, carbon monoxide and hydrogen. Most prior art reactions are based upon a flame combustion reaction in which the organic compound i~ mixed with a fuel to be burned, at high temperature, with air ~oxygen) to produce carbon dioxide and water. The problem with the latter type of reaction i9, in addition to re~uiring high temperature and high heat removal, the reaction may produce undesirable side reactions and recombinations ~products of incomplete combustion or ~ICS) which could result in P~
: , .
.
.:
.
- . .
~ ~ .
~Z8fà325 the release of toxic compounds into the environment with the effluent.
A benefit of the type of reaction employed in accordance with the method of the invention is that the - reaction is endothermic. This provides stability and safety ~ince heat is not released from the reac~ion and therefore the structural parts of the reactor are maintained at a lower temperature than they would be if the reaction were exothermic, as is the case with the combustion method. If desired, the method of the invention may be run concurrently with some oxidation reaction by adding air and/or oxygen to the input gaseous ~ixture. By regulating the amount of air introduced, it is possible to run the method as e8sentially thermally neutral.
In the ~llustrated embodiment, the gaseous mixture passed to a first reaction zone into which the gaseous mixture of organic compounds and water is passed i8 maintained at a temperature range between about 200C
and 1400C. The low temperature of the range will depend upon the temperature of the gases as they are introduced to the first reaction zone. The high temperature of the range will depend upon the reactor structure itself and the thermal limitations of the structural components. With the first reaction zone comprising an annulus which is, as will be explained below, heated from the interior thereof, the amount of heat radiated and convected from the outer surfaces of the first reaction zone will affect the temperature range of it8 operation. In the preferred embodiment, the first reaction zone is a folded annulus in which the gases flow first downwardly in the outer part and then upwardly in the coaxial inner part.
ln accordance with the invention, the first reaction zone has a labryinthine path which presents organically adsorbent surfaces to the gaseous mixture ~owing through the lab,y~ntbine path. By orgAn-callY
- '' ~Z863~:5 ads~rbent surfaces, it is meant surfaces which adsorb the organic gaseous compounds flowing through the first reaction zone, thereby slowing their flow rate and enhancing their kinetics by retaining such compounds in the zone to be fully reacted therein. By employing a labryinthine path, namely, a path that produces a tortuous and highly turbulent flow to the gases passing therethrough, sufficient mixing of the gases and therefore sufficient exposure of the organic compounds therein to the adsorbent surfaces are assured.
In accordance with the present invention, the labryinthine path and the adsorbent surfaces are selected to provide sufficient temperature, turbulent mixing, and residence time in the first reaction zone for substantially all of the gaseous organic compounds to react with the water within the first reaction zone.
By substantially all of the organic compounds, it is meant in excess of 99% and preferably in excess of 99.99% reacted. Preferably, to ensure proper turbulence and surface area, the void volume in the first reaction zone is selected to be between about 30~
and about gO~ of the total volume of the first reaction zone. Preferably, the void volume is about 75% of the total volume. As will be explained below, the void volume and tortuous path are provided by ~electing particulate material having a shape suitable to provide the above-stated characteristics.
In order to assure that the products in the first reaction zone are substantially all reacted, the amount of water added to the gaseous mixture is equal to or in excess of stoichiometry. By this terminology, it is meant that mole for mole, the amount of water is greater than is necessary to combine with 100% of the organic compounds present in the gaseous mixture. ~he preferred range is between 100% and 200% of stoichiometry, since anything greater than 200% has a ~''' ' ` '' '' ': '' ~Z86325 tendency to reduce the operating temperatures undesirably. The optimal percentage has been found to be about 131% of stoichiometry, namely, 31% in excess of stoichiometry. These levels of water assure the desired substantial reaction of the organic compounds and C02 formation in the first reaction zone, while maintaining optimal temperatures~
After reaction in the first reaction zone, the effluent from the first reaction zone is passed to a second reaction zone for further reaction. The temperature of the second reaction zone is at a higher temperature than that of the first, having a temperature range between about 750C and about 1820C.
In the second reaction zone, the rem~ining organic compounds are decomposed to carbon dioxide, carbon monoxide and hydrogen. If any oxygen is added to the gas mixture, the reaction products will also include water. As was the case in the first reaction zone, the amount of water in the second reaction zone is controlled so that it is equal to or in excess of stoichiometry in the second reaction zone. The higher temperature of the second reaction zone, together with the relatively low level of organic compounds entering the second reaction zone, assure that total and complete reaction of the organic compounds results to a level of at least 99.99~ and typically much higher.
To further assure complete reaction, the residence time of the gases in the second reaction zone is made about equal to the residence time in the first reaction zone. To do this, the flow cross-section of the second reaction zone may be made substantially larger than that of the first reaction zone to thereby increase the residence time of the flowing gases.
Preferably, the flow cross-section of the second reaction zone is about twice that of the first.
In accordance with the invention, heat is ~2~325 introduced to the reactor directly to the second reaction zone. The first reaction zone is an annulus which is positioned adjacent the second reaction zone coaxially thereof and surrounding same. AS a consequence, the heat in the second reaction zone is radiated and conducted to the first reaction zo~e to provide heating thereof.
The flow rate of the gaseous mixture introduced to the first reaction zone is, preferrably, between about two kilograms per minute and about eight kilograms per minute. The precise flow rate of the organic compound versus the water and/or oxygen will, of course, be determine~ by the stoichiometry of the chemistry involved. The flow rate of the gaseous mixture introduced to the first reaction zone is, preferrably, between about l9 cubic meters per minute and about 3.5 cubic meters per minute, depending upon the particular compound being decomposed. Typically, for a given temperature, the larger the molecule, the longer the reaction time and the higher the temperature needed to effect the desired reaction.
Referring now to FIGURE l, a typical configuration of a reactor system incorporating the invention is shown. In the system of FIGURE l, a plurality of metal drums ll, 12, 13 and 14 are shown connected to the system. It is to be understood, however, that the system of the invention and the method of the invention may be utilized in connection with a single drum or other container or source of organic materials to be decomposed, or a plurality of such sources. As shown in ~IGURE l, each drum is connected via a bidirectional flow coaxial conduit 16, 17, 18, and l9, respectively to the thermolytic detoxifier described in detail below. Each conduit has a central duct and an outer duct of annular cross section extending coaxially and coextensively with the ,' .
- ~ , . .
128~3 ~5 central duct. Flow into the respectiVe d~ums is provided through connectors 21 whereas outflow from the drums is provided through connectors 23. Outflow from the drum~ is carried through the coaxial conduits 16-19 in the inner duct of the condui,, whereas flow of hot steam and gases into the drums is through the outer annular cross-section duct of the conduit. An extension 25 is provided to couple the outer duct of the coaxial conduits 16, 17, 18, and 19 to the connectors 21. The inner ducts couple to the connectors 23.
The opposite ends of the conduits 16-19 ~rom the drums 11-14 have their central ducts all connected to an inlet conduit 27 via an extension 29. A duct 31 is connected to the outer duct of each of the coaxial conduits 16-l9 for reasons explained below. A no~mally closed valve 33 separates the inlet conduit 27 from the duct 31.
In order to volatilize the contents of the drums 11-14, the drums are heated by any suitable means. In the illustrated embodiment, a resistive heater having a plurality of coils 35 is shown surrounding the drum 11. The heater 35, together with the hot gases flowing back to the drum, raises the temperature of the drum contents to the desired level.
Similar heaters, not shown, may be provided for the other drums. Volatilization of the contents of the drums, together with the action of a turbine blower, described below, causes passage of the volatilized contents through the central duct of the conduits 16-19 through the extension 29 to the inlet conduit 27.
Water is mixed with the volatilized contents of the drums 11-14 by steam in the gas flow to and from the drums. The steam is present as a result of water addition to the reactor detoxifier 45, explained below.
The steam thus formed passes back through the outer 128~325 g annulus in each of the conduits 16-l9, depending upon the drum being operated, to pass into the drum in the space above the o~ganic material therein. In this space, the steam is mixed with the volatilized organic material and passes up through the central duct of the coaxial conduit 16, through the extension 29 and the conduit 27 and into the reactor or thermolytic detoxifier 45. ~y using the illustrated coaxial conduit arrangement, the walls of the central duct, carrying the volatilized organic compound from the drum, are kept hot enough to prevent condensation, carbonization, precipitation, and crystallization, which could plug the duct.
The internal structure of the thermol~tic detoxifier 45 is discussed in detail below. The effluent from the thermolytic detoxifier 45 passes through an outlet assembly 47 into a conduit 49. A
safety burst disk 51, designed to rupture upon the pressure of the conduit 49 exceeding a predetermined safety level, is interposed in a duct 53 communicating between the outlet 47 and a vent tube 55. The duct 49 communicates from the outlet 47 of the thermolytic detoxifier 45 to the gas-to-gas heat exchanger 43. The outlet assembly 47 can include an internal cyclone separator (not shown) to remove any fine dust carried out of thermolytic detoxifier 45.
The gas-to-gas heat exchanger 43 may be of any suitable design which serves to exchange heat from gas flowing out of the thermolytic detoxifier 45 to gas flowing into the conduit 40. After exchanging heat with such gas, the effluent passing from the conduit 49 through the gas-to-gas heat exchange~ 43 enters a conduit 57 which leads to a sorber tower 59 of suitable construction. The sorber tower 59 contains a suitable sorbent material for adsorbing any remaining impurities flowing through the conduit 57.
lZ86325 A cond~it 61 returns the effluent from the sorber tower 59 to a turbine blower 63 which provides the main motive force for producing flow in the ill~strate~ system. The outlet of the turbine blower 63 passes through a conduit 65 and through a control valve 67 into the gas-to-gas heat exchanger 43 where it is heated by the gas from the conduit 49. A normally closed valve 69 provides for venting the output of the sorber tower 59 through the turbine blower 63 via the vent 55. A pressure gauge 71 is connected to monitor the pressure across the sorber tower 59.
In order to introduce the necessary amount of water to the reactor, a water conduit 41 is provided connecting a pressurized source 37 of water to a steam inlet port 44 on the thermolytic detoxifier 45. Water flowing through the conduit 41 is heated to form steam in the coiled regions 76 and 77 of the conduit 41.
These coiled regions are formed around the conduits 57 and 61 through which the hot effluent from the thermolytic detoxifier 45 flows. Further capture of heat for the water flowing through the conduit 41 is accomplished by a plurality of coils 78 which are wrapped around the outer surface of the thermolytic detoxifier 45. Thus, by the time the water enters the thermolytic detoxifier 45 via the port 44, it is heated to the form of superheated steam and mingled with the gases entering the thermolytic detoxifier via the inlet conduit 27.
Control over the process is provided by a suitable control processor 73. Control processors utilizing various types of computers are well known in the art and therefore the control processor 73 will not be further described in detail. The operation of the control processor 73 is controlled from a suitable computer monitor 75 and touchscreen.
In operating the system illustrated in FIGURE
J2~3632S
1, each of the drums 11-14 is connected, one at a time, through the respective conduits 1~-19 to the system.
Each drum may be associated with a suitable identification code reading system, and a suitable interlock, not shown, may be used to assure that the drum may not be connected to the system until its contents are properly inputted to the control processor 73 and approved for processing.
Referring now to FIGURE 2, the specific internal details of the reactor or thermolytic detoxifier 45 may be seen in cross-section. The thermolytic detoxifier 45 comprises an outer cylindrical wall 73 of a material having sufficient structural strength at the relatively high operating temperatures described above to maintain the integrity of the reactor. Preferably, the material is type 316-L
stainless steel tubing having a thickness of four to eight millimeters wherein the longitudinal or axial dimension of the thermolytic detoxifier is about 1.8 meters and the inner diameter of the wall is about 43 centimeters. The lower end of the decomposer or reactor is closed by a circular plate 75 which is secured to the cylindrical wall 73 by means of a flange 77 extending from the wall radially outward thereof and by suitable mounting bolts 79. A flange 81 similar to the flange 77 is provided at the upper end of the cylindrical wall 77 and a circular plate 83 is bolted thereto by means of bolts 85. Sandwiched in between the plate 83 and the flange 81 and secured by the bolts 85 is a mounting ring 87. The conduit 27 (FIGURE 1) connects with the interior of the thermolytic detoxifier 45 through a port 89 located near the upper end of the cylindrical wall 73.
Extending from the ring 87 and preferably integral therewith is a cylindrical wall 91. This wall is coaxial with the wall 73 and extends downwardly from ' " ~'' ` ' -12~6325 the ring 87 about 20% of the length of the cylindrical wall 73. Interposed between the cylindrical wall 91 ~nd the cylindrical wall 73 and coaxial therewith is a cylindrical wall 93. The cylindrical wall 93 extends downwardly within the cylindrical wall 73 and terminates a distance above the plate 75 which is between about 5% and 10~ of the total axial length of the cylindrical wall 73. Preferably, the material of the ring 87, the plates 75 and 83, the cylindrical wall 91, and the cylindrical wall 93 is the same as that of the cylindrical wall 73, namely, 316-L stainless steel tubing. For a 1.8 meter length thermolytic detoxifier, the thickness of these latter elements is preferably approximately four to eight millimeters for inner diameters of about 24 centimeters for the wall 91 and 33.9 centimeters for the wall 93.
Supported on the plate 75 and extending upwardly therefrom is a cylindrical wall 95. The cylindrical wall 95 is substantially equal in diameter to the cylindrical wall 91 and is axially aligned therewith. The cylindrical wall 95 is of a length to terminate a distance below the termination of the cylindrical wall 91 so as to leave a space therebetween of a height between about 5% and about 10% of the total length of the cylindrical wall 73. Preferably, the material of which the cylindrical wall 95 is comprised is a cetamic material such as alumina or a mix of alumina and titanium oxide. Mullite (TM) tubing having a wall thickness of approximately one centimeter is a satisfactory material for the cylindrical wall 95 in a reactor of about 1.8 meters length and an inner diameter of the wall 93 of about 33.9 centimeters.
Other suitable ceramic materials for the tubing include Vycor (TM) and Pyroceram (TM).
The result of the foregoing described arrangement is a central reaction chamber 97 which is .
. , . ' .
. . , - .
lZ863Z5 surrounded by a coaxial reaction chamber 99, the latter being separated into two subchambers, an outer subchamber 101 and an inner subchamber 103. Gas entering the reactor through the port 89 may pass downwardly through the outer annulus 101, through the gap between the plate 75 and the lower end of the cylinder 93, upwardly through the inner annulus 103, through the gap between the upper end of the cylindrical wall 95 and the lower end of the cylindrical wall 91, and downwardly through the central reaction chamber 97 to exit through the port 47 in the plate 75.
The annular or outer coaxial reaction chamber 99 comprised of the subchambers 1~1 and 103 is substantially filled with particulate ceramic material indicated at 105. The material is selected to be of a size and configuration to provide a labryinthine path for gas flowing through the outer annulus 101 and inner annulus 103. In addition, the configuration and size Of the material is selected to provide the desired void volume in the space occupied by the material. The material is present in an amount sufficient to extend up to the orifice 89, thus leaving an empty annular plenum 107 at the top of the outer annulus 101 to evenly distribute the flow. Similarly, the amount of material placed in the inner annulus 103 extends to just below the upper edge of the cylindrical wall 95 to leave a plenum 109 at the upper end of the inner annulus 103 the purpose of which is to maintain a cool top flange plate and electrical feedthrough. The ceramic material utilized preferably is in the form of 1/2 inch diameter rashig rings. Also acceptable are spherical or other shaped particles of aluminum oxide.
The materials thereby provide turbulence as well as a large hot surface area exposed to the gas flow to enhance the chemical kinetics and to adsorb and thereby .'~ .
' - ' -1286:~S
increase the residence time of the hydrocarbons in the reaction chamber. This provides the desired kinetics and retention time to effect the reactions described above.
The thermolytic detoxifier 45 is heated by a plurality of elongated U-shaped hairpin shaped loops of electrical resistance heating elements 111. The heating elements 111 extend downwardly within the reaction chamber 97 a distance at least equal to half the length of the reaction chamber. The heaters are mounted in the plate 83 by a ceramic mounting fixture 113. The fixture 113 may be any suitable heat resistant insulation material, for example, quartz, alumina, molybdenum disilicide, lanthanum chromite, and lanthanum diboride. Power for the electrical heaters 111 is provided through electrical feedthroughs 115 mounted to the upper surface of the plate 83. A
radiation shield 116 is also provided just below the fixture 113. Above the heating elements there may be a metal cap (not shown) to provide a good process seal and help reduce further heat loss.
At the bottom of the reaction chamber 97, a volume of particulate material or ceramic structure 117, which can be similar to or identical to the particulate material 105, is provided. The amount of the ceramic material occupies about 5% to 15% of the length of the reaction chamber 97, remaining out of contact with the heating elements 117. The hot gases passing out of the reaction chamber 97 through the vent 47 heat the ceramic material 117. This retained heat is transferred to the ceramic material at the lower end of the annulus 99 for greater heating efficiency thus serving both as a heat recuperator and controlled gas quenching system. The heat within the chamber 97 also heats the cylinder 95 and is radiated and thermally conducted into the ceramic particulate material in the annular reaction zone 99. The flow cross-section of the central reaction chamber is about double that of the annulus 101 and of the annulus 103 to provide the desired residence time.
In operation o~ the thermolytic detoxifier 45, the mixture of gaseous organic compounds and steam (and possibly oxygen) is fed into the reactor through the port 89 and passes downwardly over the material in the outer annulus lOl and back upwardly through the material in the annulus 103. In this region, the hydrocarbons are retained on the hot adsorbent surfaces of the particulate material for a time sufficient to produce the above-descrihed reaction. In addition, the configuration of the particulate material provides sufficient turbulence for adequate mixing and to assure that the organic compounds are brought into contact with the surfaces and with the steam to effect the reaction. The decomposition of the organic compounds is at least about 99% by the time the gas enters the central reactor 97 through the gap between the cylindrical wall 91 and the cylindrical wall 95. In the reactor chamber 97, the gases encounter their highest temperature which then assures complete (at least 99.99%) reaction of the organic compounds, producing the final relatively harmless effluent. The effluent is then passed out of the port 47 for processing as described above.
Referring now to FIGURE 3, a graph depicting temperature variation within the reactor is shown. In addition, the amount of carbon monoxide measured in the source drum is also shown. All parameters measured are graphed with respect to time and for an organic waste consisting of substantially all cyclohexanone.
It may be seen that the temperature in the core or chamber 97 varies from a low of just below 1600F (785C) to a high of about 1850F
(10100C). Temperatures of the outer wall are shown as measured in three different places, a high location at about the level of the gap between the wall 95 and the wall 109, a low level near the lower end of the wall 93, and a mid level approximately half-way between the foregoing two points. Finally, it may be seen that the level of carbon monoxide substantially increases just after beginning operation as the contents of the drum volatilize due to heating. The cazbon monoxide level gradually drops, finally reaching zero after just over
2 1/2 hours of processing. By sensing the zero level of carbon monoxide, the completion of the processing of the contents of the drum may be determined~
The addition of excess water substantially lowers the levels of carbon monoxide and makes environmental control of vent gases easier. Figure 4 shows that excess water has a prompt effect on reducing carbon monoxide. The right hand scale represents carbon monoxide percentage whereas the other lines relate to the left hand scale of temperature.
The following examples are set out to further illustrate the operation of the invention. They are not intended to limit the scope of the invention which is solely defined by the claims set out below.
. " : , . -. . . .
' ~ . ' " '' : ' - , ' 128~3 ~5 Eor a mixt~re of equal parts CgHlo and CH30H (Xylene and Methanol) processed at a rate of five 55 gallon drums per day, using water addition at 131% of stoichiometry~
produces greater than 99.99~ conversion to carbon dioxide, carbon monoxide, and hyd~ogen under the following mass flow conditions (in kilograms per minute):
P~essure ol vent ~2Q ~2 ~2 ~2 NM3/~1 C. !KPA~
Drum EvapØ57 0 0 0 0 0.18 107 -6.5 0 Recycle .00 0.40 0.05 1.21 0.10 2.12 871 -6.5 Decomposer In 0.57 1.26 0.10 1.13 0.14 3.95 843 -9.4 Decomposer Out .00 0.25 0.~1 1.95 0.19 5.14 545 ~16.2 Turbine Out .00 0.25 0.61 1.95 0.19 5.14 115 +8.1 Heat ~xch.
Out.00 0.91 0.12 2.72 0.22 5.14 315 Vent.00 0.50 0.12 1.51 0.12 3.04 115 +0.5 Water In.00 1.26 0 0 01.58 91 -6.5 Drum In .00 1.26 1.13 1.13 0.14 3.40 298 -8.1.
.. . . .
.. . . . .
.
. "' ~ ' ' ' ' .
' .
Exam~le I I
For a mixture of equal parts CH30H and C13C-CH3, and a rate set at five/drums/day, the following mass flow conditions in pounds per minute were àetermined. A
stoichiometric amount of water was used. The result was in excess of 99.99~ conversion to carbon dioxide, 5 hydrogen and hydrogen chloride.
% Vol tream ~olvent ~Q ~2 ~ ~, NM3/M
Drum Evap. 0.57 0 0 0 0 1.24 0 Recycle .00 0 1.78 0.20 1.484.1 27.4 Decomposer In 0.57 0.31 1.78 0.20 1.484.57 26.8 Decomposer Out .00 0 2.28 0.2S 1.85 5.15 27.5 Turbine Out .00 0 2.28 0.29 1.85 5.15 27.5 Vent .00 0 0.46 0.05 0.37 1.03 27.6 Water In .00 0.31 0 0 0 0.39 0 Drum In .00 0.31 1.78 0.201.48 4.49 25.6.
12~36325 Exa~le I I I
For equal parts methanol and xylene, and a rate set at five drums/day, the following conditions were observed to produce 99.99~ conversion to carbon dioxide and hydrogen.
A stoichiometric amount of water was used.
P~essure Stream SolYent H~O sn C2 ~ ~M3/M C. li~-H~O) Drum Evap. 0.57 0 0 0 0 0.18107 -6.5 Recycle 0 0 1.13 0.22 0.08 2.84 871 -6.5 I DecompOSer In 0.57 0.66 1.13 0.22 0.08 3.89 288 -9.4 Decomposer Out 0 0 2.04 0.40 0.15 5.14 1315 -16.2 Turbine Out 0 0 2.04 0.40 0.15 5.14 60 +8.1 Vent 0 0 0.91 0.18 0.06 2.30 115 ~0.5 Water In 0 0.66 0 0 0 0.8591 -6.5 Drum In 0 0.66 1.13 0.22 0.08 3.67 298 -8.1 , 86 ~ 5 It may be seen, therefore, that the invention provides an improved method and apparatus for decomposing organic compounds. The organic compounds are converted into carbon di~xide, carbon monoxide, water, and hydrogen with better than 99.99~ destruction levels. High heating efficiency is attaine~ with high throughput in a relatively small size reactor. Free radical chemistry side reactions in flame combustion reactions which may produce carcinogens in vent gases are eliminated. The system operates at essentially atmospheric pressure with no expensive high maintenance compressors or heavy walled high pressure vessels.
Waste handling parts of equipment are operated below atmospheric in order to prevent waste leakage outward in case of piping or equipment leakage. The vent gas -can be used as a synthetic fuel gas to achieve power recovery in small gas engines or turbines, as a feedstock for chemical manufacture, or as a boiler or furnace fuel.
Various modifications of the invention in addition to those shown and described herein will become apparent to those skilled in the art from the foregoing description. Such modifications are intended to fall within the ~cope of the appended claims.
, . - . .
,' ' ` : ' ` - `:
.
The addition of excess water substantially lowers the levels of carbon monoxide and makes environmental control of vent gases easier. Figure 4 shows that excess water has a prompt effect on reducing carbon monoxide. The right hand scale represents carbon monoxide percentage whereas the other lines relate to the left hand scale of temperature.
The following examples are set out to further illustrate the operation of the invention. They are not intended to limit the scope of the invention which is solely defined by the claims set out below.
. " : , . -. . . .
' ~ . ' " '' : ' - , ' 128~3 ~5 Eor a mixt~re of equal parts CgHlo and CH30H (Xylene and Methanol) processed at a rate of five 55 gallon drums per day, using water addition at 131% of stoichiometry~
produces greater than 99.99~ conversion to carbon dioxide, carbon monoxide, and hyd~ogen under the following mass flow conditions (in kilograms per minute):
P~essure ol vent ~2Q ~2 ~2 ~2 NM3/~1 C. !KPA~
Drum EvapØ57 0 0 0 0 0.18 107 -6.5 0 Recycle .00 0.40 0.05 1.21 0.10 2.12 871 -6.5 Decomposer In 0.57 1.26 0.10 1.13 0.14 3.95 843 -9.4 Decomposer Out .00 0.25 0.~1 1.95 0.19 5.14 545 ~16.2 Turbine Out .00 0.25 0.61 1.95 0.19 5.14 115 +8.1 Heat ~xch.
Out.00 0.91 0.12 2.72 0.22 5.14 315 Vent.00 0.50 0.12 1.51 0.12 3.04 115 +0.5 Water In.00 1.26 0 0 01.58 91 -6.5 Drum In .00 1.26 1.13 1.13 0.14 3.40 298 -8.1.
.. . . .
.. . . . .
.
. "' ~ ' ' ' ' .
' .
Exam~le I I
For a mixture of equal parts CH30H and C13C-CH3, and a rate set at five/drums/day, the following mass flow conditions in pounds per minute were àetermined. A
stoichiometric amount of water was used. The result was in excess of 99.99~ conversion to carbon dioxide, 5 hydrogen and hydrogen chloride.
% Vol tream ~olvent ~Q ~2 ~ ~, NM3/M
Drum Evap. 0.57 0 0 0 0 1.24 0 Recycle .00 0 1.78 0.20 1.484.1 27.4 Decomposer In 0.57 0.31 1.78 0.20 1.484.57 26.8 Decomposer Out .00 0 2.28 0.2S 1.85 5.15 27.5 Turbine Out .00 0 2.28 0.29 1.85 5.15 27.5 Vent .00 0 0.46 0.05 0.37 1.03 27.6 Water In .00 0.31 0 0 0 0.39 0 Drum In .00 0.31 1.78 0.201.48 4.49 25.6.
12~36325 Exa~le I I I
For equal parts methanol and xylene, and a rate set at five drums/day, the following conditions were observed to produce 99.99~ conversion to carbon dioxide and hydrogen.
A stoichiometric amount of water was used.
P~essure Stream SolYent H~O sn C2 ~ ~M3/M C. li~-H~O) Drum Evap. 0.57 0 0 0 0 0.18107 -6.5 Recycle 0 0 1.13 0.22 0.08 2.84 871 -6.5 I DecompOSer In 0.57 0.66 1.13 0.22 0.08 3.89 288 -9.4 Decomposer Out 0 0 2.04 0.40 0.15 5.14 1315 -16.2 Turbine Out 0 0 2.04 0.40 0.15 5.14 60 +8.1 Vent 0 0 0.91 0.18 0.06 2.30 115 ~0.5 Water In 0 0.66 0 0 0 0.8591 -6.5 Drum In 0 0.66 1.13 0.22 0.08 3.67 298 -8.1 , 86 ~ 5 It may be seen, therefore, that the invention provides an improved method and apparatus for decomposing organic compounds. The organic compounds are converted into carbon di~xide, carbon monoxide, water, and hydrogen with better than 99.99~ destruction levels. High heating efficiency is attaine~ with high throughput in a relatively small size reactor. Free radical chemistry side reactions in flame combustion reactions which may produce carcinogens in vent gases are eliminated. The system operates at essentially atmospheric pressure with no expensive high maintenance compressors or heavy walled high pressure vessels.
Waste handling parts of equipment are operated below atmospheric in order to prevent waste leakage outward in case of piping or equipment leakage. The vent gas -can be used as a synthetic fuel gas to achieve power recovery in small gas engines or turbines, as a feedstock for chemical manufacture, or as a boiler or furnace fuel.
Various modifications of the invention in addition to those shown and described herein will become apparent to those skilled in the art from the foregoing description. Such modifications are intended to fall within the ~cope of the appended claims.
, . - . .
,' ' ` : ' ` - `:
.
Claims (11)
PROPERTY OR PRIVILEGE IS CLAIMED ARE DEFINED AS FOLLOWS:
1. A method for noncombustively decomposing organic compounds, comprising passing a gaseous mixture of the organic compounds and water into a reactor which includes a reaction zone having a temperature range between about 200°C and 1820°C
to noncombustively decompose the organic compounds in the gaseous mixture, maintaining the ratio of water to organic compounds present in said gaseous mixture in said reaction zone such that the amount of water is greater than the stoichiometric amount necessary to combine with 100% of the organic compounds present in the gaseous mixture, and maintaining a residence time and mixing of said gaseous mixture and said water in said reaction zone to react substantially all of said organic compounds with said water to produce carbon monoxide and hydrogen as reaction product.
to noncombustively decompose the organic compounds in the gaseous mixture, maintaining the ratio of water to organic compounds present in said gaseous mixture in said reaction zone such that the amount of water is greater than the stoichiometric amount necessary to combine with 100% of the organic compounds present in the gaseous mixture, and maintaining a residence time and mixing of said gaseous mixture and said water in said reaction zone to react substantially all of said organic compounds with said water to produce carbon monoxide and hydrogen as reaction product.
2. A method according to claim 1 wherein the amount of water in said gaseous mixture is about 131% of stoichiometry.
3. A method according to claim 1 wherein the organic compound is a liquid, and wherein the liquid organic compound is first volatilized before passing it into said reaction zone.
4. A method according to claim 1 wherein oxygen is introduced to said reaction zone in an amount sufficient to maintain the reactions therein substantially thermally neutral but in an amount insufficient to support self-sustaining combustion in said reaction zone.
5. A method according to claim 1 wherein said reaction zone comprises, a first reaction zone having a temperature range between about 200°C and 1400°C, said first reaction zone having a labyrinthine path presenting organically adsorbant surfaces to the gaseous mixture to provide a residence time in said first reaction zone sufficient to react substantially all of said gaseous organic compounds with said water, and wherein effluent from said first reaction zone is passed to a second reaction zone having a temperature range between about 750° and 1820°C.
6. A method according to claim 5 wherein said second reaction zone is maintained at a higher temperature than said first reaction zone.
7. A method according to claim 5 wherein said first reaction zone is maintained within at least two different temperature ranges including a first sub-zone having a temperature range between about 150°C and about 1100°C, and a second sub-zone having a temperature range between about 1000°C and about 1700°C, said second sub-zone being hotter than said first sub-zone.
8. A method according to claim 5 wherein said first reaction zone has a void volume between about 30% and about 90% of the total volume of said zone.
9. A method according to claim 5 wherein said first volume zone has a void volume about 75% of the total volume.
10. A method according to claim 5 wherein the gaseous mixture is introduced to the first reaction zone at a rate of between about two kilograms per minute and about eight kilograms per minute.
11. A method according to claim 5 wherein the flow rate of the gaseous mixture introduced to the first reaction zone is between about 3.5 cubic meters per minute and about 19 cubic meters per minute.
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US90323586A | 1986-09-03 | 1986-09-03 | |
| US903,235 | 1986-09-03 | ||
| US07/089,573 US4874587A (en) | 1986-09-03 | 1987-08-26 | Hazardous waste reactor system |
| US089,573 | 1987-08-26 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1286325C true CA1286325C (en) | 1991-07-16 |
Family
ID=26780722
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000545997A Expired - Lifetime CA1286325C (en) | 1986-09-03 | 1987-09-02 | Hazardous waste reactor system |
Country Status (16)
| Country | Link |
|---|---|
| US (1) | US4874587A (en) |
| EP (1) | EP0325596B1 (en) |
| JP (1) | JP2754509B2 (en) |
| KR (1) | KR950013972B1 (en) |
| CN (1) | CN87106273A (en) |
| AT (1) | ATE88258T1 (en) |
| AU (1) | AU604761B2 (en) |
| CA (1) | CA1286325C (en) |
| DE (1) | DE3785455T2 (en) |
| DK (1) | DK239688D0 (en) |
| IL (1) | IL83728A (en) |
| IN (1) | IN170401B (en) |
| MX (1) | MX167809B (en) |
| NO (1) | NO881922L (en) |
| WO (1) | WO1988001711A1 (en) |
| ZA (1) | ZA876557B (en) |
Families Citing this family (42)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5186219A (en) * | 1984-11-08 | 1993-02-16 | Earth Resources Consultants, Inc. | Cylinder rupture vessel |
| KR880010810A (en) * | 1987-03-18 | 1988-10-24 | 제이.엘.더머 | Waste disposal system |
| SE464686B (en) * | 1988-11-30 | 1991-06-03 | Boliden Contech Ab | PROCEDURES FOR DISPOSAL OF DIOXINES AND SIMILAR EXTREMELY TOXIC ORGANIC POLLUTANTS FROM A GAS |
| US5730947A (en) * | 1991-01-24 | 1998-03-24 | Societe Francaise De Thermolyse | System and process for vacuum thermolysis treatment of liquid or gas products the disposal of which is detrimental to the environment |
| ATE163474T1 (en) * | 1991-04-15 | 1998-03-15 | Scient Ecology Group Inc | HEAT EXCHANGER FOR VERY HIGH TEMPERATURE |
| US5536488A (en) * | 1991-07-01 | 1996-07-16 | Manufacturing And Technology Conversion | Indirectly heated thermochemical reactor processes |
| US5292695A (en) * | 1992-11-18 | 1994-03-08 | Synthetica Technologies, Inc. | Process for reactivating particulate adsorbents |
| WO1994020149A1 (en) * | 1993-03-08 | 1994-09-15 | The Scientific Ecology Group, Inc. | Method and system for detoxifying solid waste |
| WO1994020205A1 (en) * | 1993-03-08 | 1994-09-15 | The Sientific Ecology Group, Inc. | Method and system for steam-reforming of liquid or slurry feed materials |
| US5370715A (en) * | 1993-04-27 | 1994-12-06 | Kortzeborn; Robert N. | Waste destructor and method of converting wastes to fluid fuel |
| US5474114A (en) | 1993-05-28 | 1995-12-12 | Earth Resources Corporation | Apparatus and method for controlled penetration of compressed fluid cylinders |
| US6267931B1 (en) * | 1994-02-03 | 2001-07-31 | Earth Resources Corporation | Reconfigurable waste treatment system |
| US5582800A (en) * | 1994-12-28 | 1996-12-10 | Scientific Ecology Group | Method and system for removal of harmful heteroatoms in gaseous waste streams |
| US5614156A (en) * | 1995-02-08 | 1997-03-25 | Wang; Chi S. | Ultra-pyrolysis reactor for hazardous waste destruction |
| US5550311A (en) * | 1995-02-10 | 1996-08-27 | Hpr Corporation | Method and apparatus for thermal decomposition and separation of components within an aqueous stream |
| NL9500479A (en) * | 1995-03-10 | 1996-10-01 | Iwaco B V | Method of treating combustion residues |
| US5909654A (en) * | 1995-03-17 | 1999-06-01 | Hesboel; Rolf | Method for the volume reduction and processing of nuclear waste |
| US5672278A (en) * | 1995-05-05 | 1997-09-30 | The Scientific Ecology Group. Inc. | Method and system for suppression of foam of waste streams |
| US5638609A (en) * | 1995-11-13 | 1997-06-17 | Manufacturing And Technology Conversion International, Inc. | Process and apparatus for drying and heating |
| US5900216A (en) * | 1996-06-19 | 1999-05-04 | Earth Resources Corporation | Venturi reactor and scrubber with suckback prevention |
| US5879566A (en) * | 1997-02-03 | 1999-03-09 | The Scientific Ecology Group, Inc. | Integrated steam reforming operation for processing organic contaminated sludges and system |
| US5831143A (en) * | 1997-04-15 | 1998-11-03 | The Scientific Ecology Group, Inc. | Method for detecting hydrogen in waste compounds |
| US5809911A (en) * | 1997-04-16 | 1998-09-22 | Allied Technology Group, Inc. | Multi-zone waste processing reactor system |
| US6164344A (en) * | 1997-07-28 | 2000-12-26 | Earth Resources Corporation | Sealable recovery vessel system and method for accessing valved containers |
| US5868174A (en) * | 1997-07-28 | 1999-02-09 | Earth Resources Corporation | System for accessing and extracting contents from a container within a sealable recovery vessel |
| US20030022035A1 (en) * | 1997-11-07 | 2003-01-30 | Galloway Terry R. | Process and system for converting carbonaceous feedstocks into energy without greenhouse gas emissions |
| US6126906A (en) * | 1998-06-18 | 2000-10-03 | Kanken Techno Co., Ltd. | Apparatus for removing harmful components in a semiconductor exhaust gas |
| US6482367B1 (en) | 1998-06-18 | 2002-11-19 | Kanken Techno Co., Ltd. | Method and apparatus for removing harmful components in an exhaust gas |
| US6250236B1 (en) | 1998-11-09 | 2001-06-26 | Allied Technology Group, Inc. | Multi-zoned waste processing reactor system with bulk processing unit |
| CA2370069C (en) * | 2001-02-05 | 2009-06-02 | Honda Giken Kogyo Kabushiki Kaisha | Vehicular two-wheel drive and four-wheel drive switching system |
| US7220502B2 (en) * | 2002-06-27 | 2007-05-22 | Intellergy Corporation | Process and system for converting carbonaceous feedstocks into energy without greenhouse gas emissions |
| US7132183B2 (en) * | 2002-06-27 | 2006-11-07 | Intellergy Corporation | Process and system for converting carbonaceous feedstocks into energy without greenhouse gas emissions |
| US20040186339A1 (en) * | 2003-03-21 | 2004-09-23 | Galloway Terry R. | System and method of capturing and destroying organic hazardous agents released within an enclosed space |
| WO2007103283A2 (en) * | 2006-03-02 | 2007-09-13 | Shaw Waste Solutions, Llc | Improved steam reformation system |
| US7854775B2 (en) | 2006-05-12 | 2010-12-21 | InEn Tec, LLC | Combined gasification and vitrification system |
| US9206364B2 (en) | 2006-05-12 | 2015-12-08 | Inentec Inc. | Gasification system |
| US8118892B2 (en) * | 2006-05-12 | 2012-02-21 | Inentec Llc | Gasification system |
| US20090149996A1 (en) * | 2007-12-05 | 2009-06-11 | Applied Materials, Inc. | Multiple inlet abatement system |
| US9222039B2 (en) | 2008-01-14 | 2015-12-29 | Inentec Inc. | Grate for high temperature gasification systems |
| CN103528066B (en) * | 2012-07-05 | 2016-01-27 | 蒋华俊 | Refuse disposal installation |
| DE102014012436B3 (en) * | 2014-08-18 | 2015-07-16 | Anatoly Borodin | Two-stage thermochemical process for the production of hydrogen and a reactor for carrying out the production process |
| DE102022212861A1 (en) * | 2022-11-30 | 2024-06-06 | hollomet Gesellschaft mit beschränkter Haftung | Process for the aftertreatment of an exhaust gas from a pyrolysis reaction |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS50108769A (en) * | 1974-02-06 | 1975-08-27 | ||
| DE2428555A1 (en) * | 1974-06-14 | 1976-01-02 | Hoechst Ag | METHOD FOR REMOVAL OF HYDROCARBONS |
| US4351806A (en) * | 1980-11-18 | 1982-09-28 | The United States Of America As Represented By The United States Department Of Energy | Catalytic cartridge SO3 decomposer |
| US4414906A (en) * | 1981-08-24 | 1983-11-15 | General Dynamics, Pomona Division | Fuel cartridge and burner |
| US4688495A (en) * | 1984-12-13 | 1987-08-25 | In-Process Technology, Inc. | Hazardous waste reactor system |
| SE453120B (en) * | 1984-12-28 | 1988-01-11 | Lumalampan Ab | DEVICE FOR COMBUSTION OF EXHAUSTED GASES OF DISPOSITION OR LIKE ALL THE CARBAT WATER |
-
1987
- 1987-08-26 US US07/089,573 patent/US4874587A/en not_active Expired - Lifetime
- 1987-09-01 IL IL83728A patent/IL83728A/en not_active IP Right Cessation
- 1987-09-02 ZA ZA876557A patent/ZA876557B/en unknown
- 1987-09-02 AU AU79672/87A patent/AU604761B2/en not_active Expired
- 1987-09-02 DE DE8787906003T patent/DE3785455T2/en not_active Expired - Lifetime
- 1987-09-02 KR KR1019880700476A patent/KR950013972B1/en not_active IP Right Cessation
- 1987-09-02 WO PCT/US1987/002192 patent/WO1988001711A1/en active IP Right Grant
- 1987-09-02 JP JP62505523A patent/JP2754509B2/en not_active Expired - Lifetime
- 1987-09-02 AT AT87906003T patent/ATE88258T1/en not_active IP Right Cessation
- 1987-09-02 EP EP87906003A patent/EP0325596B1/en not_active Expired - Lifetime
- 1987-09-02 CA CA000545997A patent/CA1286325C/en not_active Expired - Lifetime
- 1987-09-02 IN IN635/MAS/87A patent/IN170401B/en unknown
- 1987-09-03 CN CN198787106273A patent/CN87106273A/en active Pending
- 1987-09-03 MX MX008099A patent/MX167809B/en unknown
-
1988
- 1988-05-02 NO NO881922A patent/NO881922L/en unknown
- 1988-05-03 DK DK239688A patent/DK239688D0/en not_active Application Discontinuation
Also Published As
| Publication number | Publication date |
|---|---|
| DK239688A (en) | 1988-05-03 |
| CN87106273A (en) | 1988-03-30 |
| IL83728A (en) | 1990-09-17 |
| EP0325596B1 (en) | 1993-04-14 |
| JPH01503763A (en) | 1989-12-21 |
| EP0325596A4 (en) | 1990-10-24 |
| US4874587A (en) | 1989-10-17 |
| ZA876557B (en) | 1988-03-07 |
| JP2754509B2 (en) | 1998-05-20 |
| DE3785455T2 (en) | 1993-08-12 |
| KR880701853A (en) | 1988-11-05 |
| WO1988001711A1 (en) | 1988-03-10 |
| DK239688D0 (en) | 1988-05-03 |
| EP0325596A1 (en) | 1989-08-02 |
| DE3785455D1 (en) | 1993-05-19 |
| NO881922D0 (en) | 1988-05-02 |
| IN170401B (en) | 1992-03-21 |
| IL83728A0 (en) | 1988-02-29 |
| AU604761B2 (en) | 1991-01-03 |
| NO881922L (en) | 1988-06-24 |
| ATE88258T1 (en) | 1993-04-15 |
| AU7967287A (en) | 1988-03-24 |
| KR950013972B1 (en) | 1995-11-18 |
| MX167809B (en) | 1993-04-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA1286325C (en) | Hazardous waste reactor system | |
| EP0785975B1 (en) | Improvements in the combustion and utilisation of fuel gases | |
| US4315893A (en) | Reformer employing finned heat pipes | |
| TW321713B (en) | ||
| US5762009A (en) | Plasma energy recycle and conversion (PERC) reactor and process | |
| CN103648972A (en) | Method and apparatus for producing synthesis gas | |
| CA1257478A (en) | Process and equipment for the generation of a product gas containing hydrogen and carbon oxides | |
| PL110558B1 (en) | Reactor for partial burning particulated solid coal fuel | |
| EP0002011B1 (en) | Method and apparatus for producing carbon black | |
| US5904910A (en) | Method for producing sulfur and hydrogen from a gaseous stream containing hydrogen sulfide and ammonia | |
| US5308587A (en) | Cooled sulphur furnace bypass system | |
| EP2705122B1 (en) | Procedure and installation for plasma heat treatment of a gas mixture | |
| JPS63197534A (en) | Reaction device | |
| CN207091007U (en) | A kind of nitrogen monoxide generating device | |
| CN205079244U (en) | Burning of oil gas heating power and emission controlling means | |
| RU2115065C1 (en) | Method and device for obtaining heated heat carrier | |
| EP0430379B1 (en) | Chemical reactor | |
| Wojciechowki et al. | Swingtherm-a new economic process for the catalytic burning of flue gases | |
| WO1990001367A1 (en) | Thermolytic detoxification reactor system | |
| JP2005500236A (en) | Catalytic reactor and method for producing high purity steam | |
| JPS6287240A (en) | Endothermic reactor | |
| AU698257B2 (en) | Improvements in the combustion and utilisation of fuel gases | |
| GB1530314A (en) | Fluid-wall reactors and their utilization in high temperature chemical reaction processes | |
| GB2158986A (en) | Method and apparatus for burning radioactive organic waste | |
| CN114322586A (en) | Laboratory sintering tail gas clean-up system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |